US20030037679A1 - Integrated compressor drier apparatus - Google Patents
Integrated compressor drier apparatus Download PDFInfo
- Publication number
- US20030037679A1 US20030037679A1 US10/257,463 US25746302A US2003037679A1 US 20030037679 A1 US20030037679 A1 US 20030037679A1 US 25746302 A US25746302 A US 25746302A US 2003037679 A1 US2003037679 A1 US 2003037679A1
- Authority
- US
- United States
- Prior art keywords
- liquid
- rotary compressor
- compressed gas
- compressor system
- absorber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000007788 liquid Substances 0.000 claims abstract description 149
- 239000006096 absorbing agent Substances 0.000 claims abstract description 49
- 238000000926 separation method Methods 0.000 claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims description 8
- 239000002826 coolant Substances 0.000 claims description 4
- 239000000314 lubricant Substances 0.000 claims description 4
- 238000010926 purge Methods 0.000 claims description 3
- 238000000034 method Methods 0.000 description 4
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 238000007605 air drying Methods 0.000 description 1
- WYTGDNHDOZPMIW-RCBQFDQVSA-N alstonine Natural products C1=CC2=C3C=CC=CC3=NC2=C2N1C[C@H]1[C@H](C)OC=C(C(=O)OC)[C@H]1C2 WYTGDNHDOZPMIW-RCBQFDQVSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/263—Drying gases or vapours by absorption
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C29/00—Component parts, details or accessories of pumps or pumping installations, not provided for in groups F04C18/00 - F04C28/00
- F04C29/0092—Removing solid or liquid contaminants from the gas under pumping, e.g. by filtering or deposition; Purging; Scrubbing; Cleaning
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C29/00—Component parts, details or accessories of pumps or pumping installations, not provided for in groups F04C18/00 - F04C28/00
- F04C29/04—Heating; Cooling; Heat insulation
- F04C29/042—Heating; Cooling; Heat insulation by injecting a fluid
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04C—ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT MACHINES FOR LIQUIDS; ROTARY-PISTON, OR OSCILLATING-PISTON, POSITIVE-DISPLACEMENT PUMPS
- F04C18/00—Rotary-piston pumps specially adapted for elastic fluids
- F04C18/08—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing
- F04C18/12—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing of other than internal-axis type
- F04C18/14—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing of other than internal-axis type with toothed rotary pistons
- F04C18/16—Rotary-piston pumps specially adapted for elastic fluids of intermeshing-engagement type, i.e. with engagement of co-operating members similar to that of toothed gearing of other than internal-axis type with toothed rotary pistons with helical teeth, e.g. chevron-shaped, screw type
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S55/00—Gas separation
- Y10S55/17—Compressed air water removal
Definitions
- the present invention relates to improvements in rotary compressor systems particularly adapted to provide clean dry compressed gas at a discharge point therefrom.
- the present invention provides a rotary compressor system utilising a liquid therein, said rotary compressor system including a driven rotary compressor unit adapted to receive gas to be compressed, a separator vessel arranged to receive compressed gas and entrained liquid from said compressor unit and for collecting said liquid therein, means for returning said liquid to a lower pressure zone of said compressor unit and to a moisture absorber, compressed gas flow leaving a separation zone of said separator vessel being passed to the moisture absorber to be contacted by a flow of said liquid whereby moisture in said compressed gas flow is transferred to said liquid.
- the present invention provides a rotary compressor system utilising a liquid therein, said rotary compressor system including a driven rotary compressor unit adapted to receive gas to be compressed, a separator vessel arranged to receive compressed gas and entrained liquid from said compressor unit and for collecting said liquid therein, means for returning said liquid to a lower pressure zone of said compressor unit and to a moisture absorber, compressed gas flow leaving a separation zone of said separator vessel being passed through a first cooler means to condense at least a proportion of moisture carried by said compressed gas to be collected and discharged from said compressed gas flow prior to said compressed gas flow being passed to the moisture absorber to be contacted by a flow of said liquid whereby said compressed gas flow is further dried with moisture in said compressed gas being transferred to said liquid.
- the liquid referred to in the aforesaid paragraphs is often a lubricant but does not necessarily need to be.
- FIGS. 1, 2, 4 , 7 , 8 , 9 and 10 are schematic illustrations of preferred embodiments of compressor systems including gas drier equipment according to the present invention
- FIGS. 3, 5, 6 , 10 a , 10 b and 11 show schematically potential alternatives or changes to the compressor systems shown in the other drawings.
- a compressor system may include a compressor unit 10 driven by a motor 11 which receives a gas (typically air) to be compressed at 12 via an inlet valve 7 .
- the rotary compressor unit 10 may be a screw compressor of any known configuration or in fact any other form of rotary compressor.
- the system further includes a separator vessel 13 receiving compressed gas and entrained liquid via line 14 with a preliminary separation of gas and liquid occurring therein. The liquid is collected in a lower region of the vessel 13 and returned via line 15 , a liquid or lubricant filter 6 , and a liquid cooler 16 , to a lower pressure region of the compressor unit 10 . Compressed gas leaves the vessel 13 via a preliminary filter means 17 and a minimum pressure valve 18 .
- the compressor system thus described is essentially conventional in nature and within the context of this invention might be substituted by any other known similar rotary compressor system.
- the compressed gas flow leaving the separator vessel 13 is conveniently cooled in a gas cooler device 19 such that at least a portion of the moisture is cooled, condensed, collected and drained away at 20 from the system.
- the cool humid compressed gas flow is then passed via line 21 to an absorption column 22 where a shower of cool dry liquid is falling. As the compressed gas flow passes upwardly through this shower, moisture is absorbed into the liquid flow conveniently originating via diverting a portion of the liquid flow in line 15 through a line 23 and thereafter passing same through a further liquid cooler 24 prior to delivering same to the absorption column 22 .
- the diverted flow might be after the cooler 16 with or without further cooling.
- the liquid is preferably of the type which is hydrophilic in nature, that is it will absorb moisture to some degree.
- Glycol based liquids including lubricants are useful for this purpose and may include such liquid lubricants as Ingersoll Rand's “Ultra” coolant and Kuba-Summit's “Supra” coolant.
- the liquid falls to the bottom of the absorber column 22 where it is collected and conveniently passed via line 25 back to line 15 or some other lower pressure region of the compressor circuit including the compressor unit 10 .
- This liquid flow then mixes with the main liquid flow where it is heated and the absorbed moisture flashes into vapour.
- This vapour is subsequently condensed in the gas after cooler device 19 and at least partially drained away at 20 .
- the cool dry compressed gas flow leaving the absorption column 22 passes through a final filter means 26 so that no droplets of coolant can escape with the clean dry compressed gas discharge at 27 .
- the filter means 18 and 26 may typically be of the coalescent type.
- liquid purge lines 28 , 29 are operatively associated with each of the filter means 17 and 26 to return any collected liquid back to a lower pressure portion of the compressor system such as the compressor unit 10 itself. Further possible changes to the system may include integrating the absorption column 22 into the separator vessel 13 whereby a secondary vessel is not required. Alternatively, the absorption column 22 might be integrated into the air receiver tank (not shown).
- the integrated compressor drier described in the foregoing with reference to FIG. 1 attains a dewpoint of approximately 20-25° C. less than ambient. Consequently, when ambient temperature is 20° C., a dewpoint of approximately 0 to ⁇ 5° C. might be expected. For some applications a dewpoint of ⁇ 20 to ⁇ 40° C. may be desired. This may be attained in a two stage process whereby dry liquid entering the absorber column passes first through a pre-separation process to lower its relative humidity. A possible arrangement for achieving this is shown in FIG. 2. In this arrangement, compressor 10 of the liquid injected positive displacement type (e.g. screw, vane or scroll) is driven by motor 11 , which may be electric, hydraulic or internal combustion.
- motor 11 which may be electric, hydraulic or internal combustion.
- Liquid is separated in the vessel 13 and is returned via a liquid filter 6 , cooler 16 to the compressor 10 . Some of the liquid is, however, further cooled in cooler 28 before passing through an orifice 29 whereby pressure falls to atmospheric. Whilst the liquid and the compressed gas are being separated in the separator vessel 13 , the heat of compression evaporates most moisture contained in the liquid. This moisture in vapour form passes into an after cooler 19 where the compressed gas is cooled and most moisture condenses.
- a moisture separator 20 collects moisture droplets from the gas and purges them to waste.
- the compressed gas then is passed into the absorber column 22 where it contacts falling dry liquid. In passing upwards, the gas is dried and moisture is transferred to the falling liquid. Dry compressed gas leaves the absorber column through a minimum pressure valve (mpv) 18 and is discharged to a desired end use or to a receiver vessel not shown.
- mpv
- a small amount of dry air is removed from the discharge line 27 and is passed via line 30 via an orifice 31 to a stripper 32 .
- This dry compressed gas is expanded through the orifice 31 to atmospheric pressure which further dries the gas.
- This ultra dry gas then passes upwardly through a failing shower of liquid in the stripper 32 and removes moisture and further dries the liquid passing through the stripper 32 .
- the gas is then passed through line 33 back to the inlet of the compressor 10 .
- Ultra dry liquid drops to the bottom of the stripper 32 where it is pumped by pump 34 via line 35 to the top of the absorber column 22 . This ultra dry liquid falls through the absorber column removing moisture from the compressed gas, before returning via line 36 back to the compressor 10 .
- the pump 34 may be of the air driven type where compressed gas is used to power the pump as shown for example in FIG. 3.
- this compressed gas may be obtained from the dry air outlet divergent line 30 .
- the motive power of the pump is obtained from an energy source that may otherwise go to waste and no additional energy is needed.
- Such an arrangement may include an inlet valve 37 in the line 30 which is controlled by a position sensor 38 sensing the position of the larger piston 39 .
- the valve 37 when activated admits high pressure gas on to the larger piston 39 drawing the smaller piston 40 to the left. Liquid enters the pump 34 via a non return valve 41 and exits via a non return valve 42 .
- an electrical heating element or coil 43 might be installed in the liquid pool in the base of the vessel 13 . Power supply to the heating element 43 might optionally be controlled by a thermostatically operated switch 44 sensing the liquid temperature.
- FIG. 4 illustrates two possible embodiments. The first allows the liquid exiting the stripper 32 to flow via line 90 , pump 34 and cooler 28 directly to the absorber 22 . The second diverts this exiting liquid flow through a heat exchanger 91 being placed in heat exchange relationship with liquid flowing into the stripper 32 .
- FIG. 5 illustrates a multistage cross-flow absorber which might also be used.
- a pool of liquid 55 is maintained in vessel 50 with the liquid being introduced via line 51 and withdrawn via line 52 .
- Compressed air is supplied via line 53 to be bubbled through the liquid before leaving via line 54 .
- a plurality of vessels 50 might be provided such that compressed gas is successively bubbled through the fluid in each vessel via intermediary connecting lines 56 with the liquid supplied via a header pipe 57 to all vessels and withdrawn via a common pipe 58 .
- FIG. 7 For smaller machines where a relatively high moisture content is acceptable, parallel flow absorber constructions are acceptable.
- air from the moisture trap 20 enters one leg of a T-piece 60 with dry cool liquid entering the other leg. Liquid travels along the wall of a hose/pipe 61 forming an absorber 22 .
- the hose or pipe 61 may be straight, serpentine or coiled and it has sufficient length to promote good mixing of the liquid and compressed gas and to ensure the moisture in the gas is absorbed into the liquid.
- a liquid separator 62 is provided essentially similar to the moisture trap 20 , but which removes liquid droplets (together with any contained moisture) from the compressed gas.
- This liquid/moisture is returned to the compressor 10 or any lower pressure part of the compression circuit via line 63 .
- a filter means such as a coalescent type filter may be incorporated into the liquid separator 62 or in the discharge line 27 therefrom. Dry compressed gas without liquid then may be discharged via a minimum pressure valve 18 and line 27 .
- the difficulty with all cross-flow and parallel flow absorber systems is that the driest oil does not necessarily contact the driest compressed gas.
- compressed gas with a degree of moisture content enters at the bottom and as the gas rises, the gas successively contacts drier and drier liquid whereby at the discharge point, the gas is contacting the most dry or totally dry liquid.
- the most dry liquid contacts the gas with the greatest moisture content at the start of the drying process and at the end of the process, the gas is contacting liquid with the greatest moisture content. This effect may be reduced by increasing the liquid flow rate relative to the gas flow rate.
- liquid leaving the separator 13 is passed into a counter flow recuperator (heat exchanger) 64 if the tube in tube or plate type as known to those skilled in the art of heat exchange.
- the hot dry liquid is cooled by moist liquid returning from the droplet separator 60 via line 63 .
- the moist liquid is warmed by the cooling of the dry liquid.
- the liquid is returned to the screw at a convenient point in the casing of compressor 10 .
- no gas is wasted and the specific energy consumption is good.
- a pump may also be used to pump liquid directly from the absorber to the separator. This pump can be of conventional design or an ejector.
- FIG. 9 A still further possible embodiment of a compressor system according to this invention is illustrated in FIG. 9.
- moist gas enters into the bottom of the absorber 22 at 21 .
- the gas then flows upwardly contacting falling dry liquid injected via line 35 .
- Moisture is absorbed by the liquid from the gas, thereby drying the gas.
- Wet liquid is transferred via line 65 under action of the compressed gas to the stripper 32 where it enters at the top.
- the stripper 32 conveniently operates at a lower pressure than the absorber 22 and wet liquid flows downwardly within the stripper 32 .
- Dry compressed gas leaves the absorber 22 via a minimum pressure valve 18 and line 27 after conveniently passing through a filter 66 to remove any droplets of liquid therefrom.
- Part of the dry compressed gas is bled from the discharge 27 via line 30 into the stripper 32 .
- This dry gas rises through the stripper 32 , drying the liquid removing moisture before exiting via filter 67 and is discharged to atmosphere at 68 .
- Dry liquid is collected at the bottom of the stripper 32 and pumped via pump 34 to the top of the absorber 22 via line 35 .
- the pump 34 may be any conventional pumping means as discussed on earlier embodiments including a gas driven pump of the type described with reference to FIG. 3. In this latter arrangement the gas driven pump may replace orifice 31 as illustrated.
- a drier 69 of the configuration shown in FIG. 9, in combination with a typical rotary compressor configuration 70 of any known arrangement including that illustrated, will use about 15% of the gas passing through it to regenerate the liquid used as an absorber material. Due to the energy cost of compressing gas, this loss may be considered somewhat wasteful.
- Heat supplied to the heater 73 may be by electric means or may utilize heat from a compressor by passing hot compressed gas or liquid through the heater 73 acting as a heat exchanger.
- hot compressed gas via line 74 passes through the heat exchanger 73 before entering an after cooler 75 .
- hot liquid via line 74 passes firstly through the heat exchanger 73 before passing through a liquid cooler 76 as shown in FIG. 10 b .
- FIGS. 10 a and 10 b show series flow, it is also possible that the cooler 73 could be placed in a parallel flow circuit 73 b .
- the liquid flow circuit of a standard compressor system 70 may be tapped at the liquid filter as shown, for example, in FIG. 11.
- FIG. 11 illustrates the use of a novel adapter plate 85 interposed between the head 82 and can 80 . Liquid may thereby be diverted via part 86 through the heat exchanger 73 located in the drier 69 before returning through part 87 .
- a drier of this heated configuration is believed to use less than 1% of the pressurized gas flow to regenerate the liquid used as the moisture absorbent.
- compressor systems as described in the foregoing may be built as an integral construction including the compressor 70 and the drier 69 on a common support base, structure a platform or alternatively they could be built respectively on different support platforms or structures.
Abstract
Description
- The present invention relates to improvements in rotary compressor systems particularly adapted to provide clean dry compressed gas at a discharge point therefrom.
- There is increasingly a need to provide moisture free pressurized gas or air. Such moisture free pressurized gas or air is normally achieved by using various forms of gas or air drying equipment including refrigeration driers, however, such driers are expensive and complicated. The objective therefore is to provide in a simplified and inexpensive way, a rotary compressor system capable of providing clean dry compressed gas.
- Accordingly, the present invention provides a rotary compressor system utilising a liquid therein, said rotary compressor system including a driven rotary compressor unit adapted to receive gas to be compressed, a separator vessel arranged to receive compressed gas and entrained liquid from said compressor unit and for collecting said liquid therein, means for returning said liquid to a lower pressure zone of said compressor unit and to a moisture absorber, compressed gas flow leaving a separation zone of said separator vessel being passed to the moisture absorber to be contacted by a flow of said liquid whereby moisture in said compressed gas flow is transferred to said liquid.
- According to a further aspect, the present invention provides a rotary compressor system utilising a liquid therein, said rotary compressor system including a driven rotary compressor unit adapted to receive gas to be compressed, a separator vessel arranged to receive compressed gas and entrained liquid from said compressor unit and for collecting said liquid therein, means for returning said liquid to a lower pressure zone of said compressor unit and to a moisture absorber, compressed gas flow leaving a separation zone of said separator vessel being passed through a first cooler means to condense at least a proportion of moisture carried by said compressed gas to be collected and discharged from said compressed gas flow prior to said compressed gas flow being passed to the moisture absorber to be contacted by a flow of said liquid whereby said compressed gas flow is further dried with moisture in said compressed gas being transferred to said liquid.
- The liquid referred to in the aforesaid paragraphs is often a lubricant but does not necessarily need to be.
- Further preferred features and aspects of this invention may be found in the annexed patent claims which are hereby made part of this specification and from the following description given in relation to the accompanying drawings, in which:
- FIGS. 1, 2,4, 7, 8, 9 and 10 are schematic illustrations of preferred embodiments of compressor systems including gas drier equipment according to the present invention;
- FIGS. 3, 5,6, 10 a, 10 b and 11 show schematically potential alternatives or changes to the compressor systems shown in the other drawings.
- As illustrated in FIG. 1, a compressor system according to this preferred embodiment of the present invention may include a
compressor unit 10 driven by amotor 11 which receives a gas (typically air) to be compressed at 12 via aninlet valve 7. Therotary compressor unit 10 may be a screw compressor of any known configuration or in fact any other form of rotary compressor. The system further includes aseparator vessel 13 receiving compressed gas and entrained liquid vialine 14 with a preliminary separation of gas and liquid occurring therein. The liquid is collected in a lower region of thevessel 13 and returned vialine 15, a liquid orlubricant filter 6, and aliquid cooler 16, to a lower pressure region of thecompressor unit 10. Compressed gas leaves thevessel 13 via a preliminary filter means 17 and aminimum pressure valve 18. The compressor system thus described is essentially conventional in nature and within the context of this invention might be substituted by any other known similar rotary compressor system. - The compressed gas flow leaving the
separator vessel 13 is conveniently cooled in a gas cooler device 19 such that at least a portion of the moisture is cooled, condensed, collected and drained away at 20 from the system. The cool humid compressed gas flow is then passed vialine 21 to anabsorption column 22 where a shower of cool dry liquid is falling. As the compressed gas flow passes upwardly through this shower, moisture is absorbed into the liquid flow conveniently originating via diverting a portion of the liquid flow inline 15 through aline 23 and thereafter passing same through a furtherliquid cooler 24 prior to delivering same to theabsorption column 22. In an alternative arrangement the diverted flow might be after thecooler 16 with or without further cooling. In this embodiment, the liquid is preferably of the type which is hydrophilic in nature, that is it will absorb moisture to some degree. Glycol based liquids including lubricants are useful for this purpose and may include such liquid lubricants as Ingersoll Rand's “Ultra” coolant and Kuba-Summit's “Supra” coolant. - The liquid falls to the bottom of the
absorber column 22 where it is collected and conveniently passed vialine 25 back toline 15 or some other lower pressure region of the compressor circuit including thecompressor unit 10. This liquid flow then mixes with the main liquid flow where it is heated and the absorbed moisture flashes into vapour. This vapour is subsequently condensed in the gas after cooler device 19 and at least partially drained away at 20. - The cool dry compressed gas flow leaving the
absorption column 22 passes through a final filter means 26 so that no droplets of coolant can escape with the clean dry compressed gas discharge at 27. The filter means 18 and 26 may typically be of the coalescent type. Convenientlyliquid purge lines compressor unit 10 itself. Further possible changes to the system may include integrating theabsorption column 22 into theseparator vessel 13 whereby a secondary vessel is not required. Alternatively, theabsorption column 22 might be integrated into the air receiver tank (not shown). - The integrated compressor drier described in the foregoing with reference to FIG. 1 attains a dewpoint of approximately 20-25° C. less than ambient. Consequently, when ambient temperature is 20° C., a dewpoint of approximately 0 to −5° C. might be expected. For some applications a dewpoint of −20 to −40° C. may be desired. This may be attained in a two stage process whereby dry liquid entering the absorber column passes first through a pre-separation process to lower its relative humidity. A possible arrangement for achieving this is shown in FIG. 2. In this arrangement,
compressor 10 of the liquid injected positive displacement type (e.g. screw, vane or scroll) is driven bymotor 11, which may be electric, hydraulic or internal combustion. Air or other gas enters throughinlet valve 7 and a mixture of gas and liquid, after being compressed, passes to aseparator vessel 13. Liquid is separated in thevessel 13 and is returned via aliquid filter 6,cooler 16 to thecompressor 10. Some of the liquid is, however, further cooled in cooler 28 before passing through anorifice 29 whereby pressure falls to atmospheric. Whilst the liquid and the compressed gas are being separated in theseparator vessel 13, the heat of compression evaporates most moisture contained in the liquid. This moisture in vapour form passes into an after cooler 19 where the compressed gas is cooled and most moisture condenses. Amoisture separator 20 collects moisture droplets from the gas and purges them to waste. The compressed gas then is passed into theabsorber column 22 where it contacts falling dry liquid. In passing upwards, the gas is dried and moisture is transferred to the falling liquid. Dry compressed gas leaves the absorber column through a minimum pressure valve (mpv) 18 and is discharged to a desired end use or to a receiver vessel not shown. - A small amount of dry air is removed from the
discharge line 27 and is passed vialine 30 via anorifice 31 to astripper 32. This dry compressed gas is expanded through theorifice 31 to atmospheric pressure which further dries the gas. This ultra dry gas then passes upwardly through a failing shower of liquid in thestripper 32 and removes moisture and further dries the liquid passing through thestripper 32. The gas is then passed throughline 33 back to the inlet of thecompressor 10. Ultra dry liquid drops to the bottom of thestripper 32 where it is pumped bypump 34 vialine 35 to the top of theabsorber column 22. This ultra dry liquid falls through the absorber column removing moisture from the compressed gas, before returning via line 36 back to thecompressor 10. - In a modification of the embodiment shown in FIG. 2, the
pump 34 may be of the air driven type where compressed gas is used to power the pump as shown for example in FIG. 3. Conveniently, this compressed gas may be obtained from the dry air outletdivergent line 30. By this means the motive power of the pump is obtained from an energy source that may otherwise go to waste and no additional energy is needed. Such an arrangement may include aninlet valve 37 in theline 30 which is controlled by a position sensor 38 sensing the position of the larger piston 39. Thevalve 37 when activated admits high pressure gas on to the larger piston 39 drawing the smaller piston 40 to the left. Liquid enters thepump 34 via anon return valve 41 and exits via anon return valve 42. When the piston 40 has reached its extreme left position, sensor 38 stops, viavalve 37, the gas supply from theline 30 opens theoutlet valve 43. Thespring 44 then pushes pistons 39, 40 back to a right hand or start position. There are many variations of this type of air driven pump and any other version might equally be used without departing from the scope of this invention. For larger machines, it may be preferable to use a rotary pump. In such an embodiment a vane motor may be installed in theline 30 to drive via a connecting shaft, a centrifugal pump installed in theline 35. The vane motor might be replaced by a turbine, screw or rotary piston type motor without departing from the spirit of this invention. - During intermittent operation of the compressor system, it is possible that the liquid temperature in the
separator vessel 13 may not reach an optimum temperature before thecompressor 10 shuts down. To eliminate this problem, an electrical heating element orcoil 43 might be installed in the liquid pool in the base of thevessel 13. Power supply to theheating element 43 might optionally be controlled by a thermostatically operatedswitch 44 sensing the liquid temperature. - In yet another preferred embodiment of the present invention as shown in FIG. 4, it is possible to attain even lower dewpoints by operating the stripping process at high temperature. This hot stripping dries the liquid passing to the absorber column still further and allows less bled air from the
discharge line 27 vialine 30 to be used as the stripping air is hotter and as such has a greater capacity to absorb moisture. Referring to FIG. 4, theliquid cooler 28 has been moved to theline 35 leading to theabsorber column 22, i.e. after the liquid has passed through thestripper 32. Thus hot liquid enters thestripper 32 at the top. Dry gas viableed line 30, expanded and further dried is first passed through aheat exchanger 45 warming the gas. This combination of hot liquid and hot gas allows the liquid to be dried more than via the cold stripping process shown in FIG. 2 and allows the use of less dry gas bled from thedischarge line 27 vialine 30. Whilst theheat exchanger 45 is shown in this embodiment, it is clear that the dry gas inline 30 could be heated by other means such as passing a loop of thepipe forming line 30 through the hot liquid pool in theseparator vessel 13, or perhaps simply passing loops of thepipe forming line 30 around the outer shell of theseparator vessel 13. FIG. 4 illustrates two possible embodiments. The first allows the liquid exiting thestripper 32 to flow vialine 90, pump 34 and cooler 28 directly to theabsorber 22. The second diverts this exiting liquid flow through aheat exchanger 91 being placed in heat exchange relationship with liquid flowing into thestripper 32. - The description of the embodiments set out above generally describe a counter flow contact arrangement for the liquid flow and the compressed gas flow in the
absorber column 22. The nature of thestripper column 32 may be generally similar to that of theabsorber column 22. However, counter flow arrangements are not essential to the performance of this invention. Any generally known arrangements for contacting a liquid flow with a pressurized gas flow could be used although it may be apparent to those skilled in the art that some arrangements will work better than others. One potential alternative configuration is a simple cross-flow absorber as shown schematically in FIG. 5. FIG. 6 illustrates a multistage cross-flow absorber which might also be used. In FIG. 5 a pool ofliquid 55 is maintained invessel 50 with the liquid being introduced vialine 51 and withdrawn vialine 52. Compressed air is supplied vialine 53 to be bubbled through the liquid before leaving vialine 54. In FIG. 6 a plurality ofvessels 50 might be provided such that compressed gas is successively bubbled through the fluid in each vessel via intermediary connectinglines 56 with the liquid supplied via aheader pipe 57 to all vessels and withdrawn via acommon pipe 58. - For smaller machines where a relatively high moisture content is acceptable, parallel flow absorber constructions are acceptable. One such possible arrangement is shown in FIG. 7. In this embodiment, air from the
moisture trap 20 enters one leg of a T-piece 60 with dry cool liquid entering the other leg. Liquid travels along the wall of a hose/pipe 61 forming anabsorber 22. The hose orpipe 61 may be straight, serpentine or coiled and it has sufficient length to promote good mixing of the liquid and compressed gas and to ensure the moisture in the gas is absorbed into the liquid. At the end of the hose/pipe 61, aliquid separator 62 is provided essentially similar to themoisture trap 20, but which removes liquid droplets (together with any contained moisture) from the compressed gas. This liquid/moisture is returned to thecompressor 10 or any lower pressure part of the compression circuit vialine 63. If desired a filter means such as a coalescent type filter may be incorporated into theliquid separator 62 or in thedischarge line 27 therefrom. Dry compressed gas without liquid then may be discharged via aminimum pressure valve 18 andline 27. - The difficulty with all cross-flow and parallel flow absorber systems is that the driest oil does not necessarily contact the driest compressed gas. In a counter flow absorber system, compressed gas with a degree of moisture content enters at the bottom and as the gas rises, the gas successively contacts drier and drier liquid whereby at the discharge point, the gas is contacting the most dry or totally dry liquid. In a parallel flow absorber, the most dry liquid contacts the gas with the greatest moisture content at the start of the drying process and at the end of the process, the gas is contacting liquid with the greatest moisture content. This effect may be reduced by increasing the liquid flow rate relative to the gas flow rate. By pushing more liquid through the absorber, the increase in the liquid moisture content on a percentage basis is reduced, but unfortunately there is an upper limit to how much liquid can be injected into the absorber. As the liquid must be cooled, if too much liquid is injected, good absorption and low RH use is achieved but the discharge temperature of the
compression 10 falls (as more heat is' lost through the cooler). A lower discharge temperature means that less moisture is removed in theseparator 13, and so, in this condition, the moisture content of the liquid entering the absorber is too high. This problem may be overcome or at least minimized by the addition of a small extra heat exchanger orrecuperator 64 as shown in FIG. 8. - As shown in FIG. 8, liquid leaving the
separator 13 is passed into a counter flow recuperator (heat exchanger) 64 if the tube in tube or plate type as known to those skilled in the art of heat exchange. The hot dry liquid is cooled by moist liquid returning from thedroplet separator 60 vialine 63. In turn the moist liquid is warmed by the cooling of the dry liquid. By this means heat is conserved and the compressor does not run too cool. Accordingly the mass flow rate of liquid may be increased, so the discharge RH of the liquid may be kept low. - In all embodiments described thus far, the liquid is returned to the screw at a convenient point in the casing of
compressor 10. By this means no gas is wasted and the specific energy consumption is good. It is also possible to return the liquid to the inlet of the compressor, maintaining a liquid seal in the absorber by a float valve. A pump may also be used to pump liquid directly from the absorber to the separator. This pump can be of conventional design or an ejector. - A still further possible embodiment of a compressor system according to this invention is illustrated in FIG. 9. In this arrangement, moist gas enters into the bottom of the
absorber 22 at 21. The gas then flows upwardly contacting falling dry liquid injected vialine 35. Moisture is absorbed by the liquid from the gas, thereby drying the gas. Wet liquid is transferred vialine 65 under action of the compressed gas to thestripper 32 where it enters at the top. Thestripper 32 conveniently operates at a lower pressure than theabsorber 22 and wet liquid flows downwardly within thestripper 32. Dry compressed gas leaves theabsorber 22 via aminimum pressure valve 18 andline 27 after conveniently passing through afilter 66 to remove any droplets of liquid therefrom. Part of the dry compressed gas is bled from thedischarge 27 vialine 30 into thestripper 32. This dry gas rises through thestripper 32, drying the liquid removing moisture before exiting viafilter 67 and is discharged to atmosphere at 68. Dry liquid is collected at the bottom of thestripper 32 and pumped viapump 34 to the top of theabsorber 22 vialine 35. Thepump 34 may be any conventional pumping means as discussed on earlier embodiments including a gas driven pump of the type described with reference to FIG. 3. In this latter arrangement the gas driven pump may replaceorifice 31 as illustrated. A drier 69 of the configuration shown in FIG. 9, in combination with a typicalrotary compressor configuration 70 of any known arrangement including that illustrated, will use about 15% of the gas passing through it to regenerate the liquid used as an absorber material. Due to the energy cost of compressing gas, this loss may be considered somewhat wasteful. - Energy usage efficiencies may be improved by utilizing a configuration as shown in FIG. 10. Referring to FIG. 10, wet liquid leaving the
absorber 22 vialine 65 passes through a counterflow heat exchanger 71 and through aheater 73 before being injected into the top of thestripper 32 vialine 72. By this means moisture is driven off into dry gas rising through thestripper 32. Dry liquid acting as an absorber leaving thestripper 32 vialine 74 passes through the counterflow heat exchanger 71 and is cooled, which in turn provides the energy to preheat the liquid absorbent flowing to the stripper. Liquid then flows to pump 34 and is injected into theabsorber 22 vialine 35. - Heat supplied to the
heater 73 may be by electric means or may utilize heat from a compressor by passing hot compressed gas or liquid through theheater 73 acting as a heat exchanger. As shown in FIG. 10a, hot compressed gas vialine 74 passes through theheat exchanger 73 before entering an after cooler 75. Alternatively hot liquid vialine 74 passes firstly through theheat exchanger 73 before passing through a liquid cooler 76 as shown in FIG. 10b. Whilst the drawings FIGS. 10a and 10 b show series flow, it is also possible that the cooler 73 could be placed in aparallel flow circuit 73 b. Conveniently, the liquid flow circuit of astandard compressor system 70 may be tapped at the liquid filter as shown, for example, in FIG. 11. - Most compressors of this general type are filled with a spin-on
liquid filter 6 which has anouter can 80 and an inner paper (or similar)filter element 81. Liquid to be filtered enters thehead 82 at 83 and passes directly into thecan 80. It then passes through thefilter element 81 before leaving at 84. FIG. 11 illustrates the use of anovel adapter plate 85 interposed between thehead 82 and can 80. Liquid may thereby be diverted viapart 86 through theheat exchanger 73 located in the drier 69 before returning throughpart 87. A drier of this heated configuration is believed to use less than 1% of the pressurized gas flow to regenerate the liquid used as the moisture absorbent. - It will of course be appreciated that the compressor systems as described in the foregoing may be built as an integral construction including the
compressor 70 and the drier 69 on a common support base, structure a platform or alternatively they could be built respectively on different support platforms or structures.
Claims (22)
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AUPQ6829 | 2000-04-11 | ||
AUPQ6829A AUPQ682900A0 (en) | 2000-04-11 | 2000-04-11 | Integrated compressor drier apparatus |
AUPQ9997 | 2000-09-08 | ||
AUPQ9997A AUPQ999700A0 (en) | 2000-09-08 | 2000-09-08 | Integrated compressor drier apparatus |
PCT/AU2001/000403 WO2001077528A1 (en) | 2000-04-11 | 2001-04-10 | Integrated compressor drier apparatus |
Publications (2)
Publication Number | Publication Date |
---|---|
US20030037679A1 true US20030037679A1 (en) | 2003-02-27 |
US6843836B2 US6843836B2 (en) | 2005-01-18 |
Family
ID=25646296
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/257,463 Expired - Lifetime US6843836B2 (en) | 2000-04-11 | 2001-04-10 | Integrated compressor drier apparatus |
Country Status (4)
Country | Link |
---|---|
US (1) | US6843836B2 (en) |
JP (1) | JP4666871B2 (en) |
DE (1) | DE10196063B4 (en) |
WO (1) | WO2001077528A1 (en) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030106431A1 (en) * | 2000-04-11 | 2003-06-12 | Kitchener Anthony John | Compressor/drier system and absorber therefor |
US6843836B2 (en) * | 2000-04-11 | 2005-01-18 | Cash Engineering Research Pty Ltd. | Integrated compressor drier apparatus |
US20050268781A1 (en) * | 2004-06-02 | 2005-12-08 | Rdc Research Llc | Method and system for processing natural gas using a rotary screw compressor |
US20110100213A1 (en) * | 2009-10-30 | 2011-05-05 | Matthias Finkenrath | System and method for reducing moisture in a compressed air energy storage system |
CN104801157A (en) * | 2015-04-08 | 2015-07-29 | 上海理工大学 | Moisture removal device and air compressor system |
US20170082098A1 (en) * | 2015-09-21 | 2017-03-23 | Clark Equipment Company | Condensate vaporization system |
CN107983055A (en) * | 2017-12-18 | 2018-05-04 | 赵国庆 | A kind of environment-friendly boiler waste gas circulation cleaning equipment |
Families Citing this family (40)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8075668B2 (en) | 2005-03-29 | 2011-12-13 | Dresser-Rand Company | Drainage system for compressor separators |
US7343755B2 (en) * | 2006-01-04 | 2008-03-18 | Flatplate, Inc. | Gas-drying system |
US8434998B2 (en) * | 2006-09-19 | 2013-05-07 | Dresser-Rand Company | Rotary separator drum seal |
BRPI0718513B1 (en) | 2006-09-21 | 2018-10-23 | Dresser Rand Co | fluid handling set for a fluid machine |
WO2008039731A2 (en) | 2006-09-25 | 2008-04-03 | Dresser-Rand Company | Access cover for pressurized connector spool |
CA2663880C (en) | 2006-09-25 | 2015-02-10 | William C. Maier | Compressor mounting system |
CA2661925C (en) | 2006-09-25 | 2015-04-28 | Gocha Chochua | Fluid deflector for fluid separator devices |
US8079622B2 (en) | 2006-09-25 | 2011-12-20 | Dresser-Rand Company | Axially moveable spool connector |
US8061737B2 (en) | 2006-09-25 | 2011-11-22 | Dresser-Rand Company | Coupling guard system |
CA2663868C (en) | 2006-09-26 | 2015-11-10 | William C. Maier | Improved static fluid separator device |
WO2008080068A2 (en) * | 2006-12-22 | 2008-07-03 | Donaldson Company, Inc. | Gas/liquid separator assembly with preseparator and liquid filter, and methods |
US7837752B2 (en) * | 2007-12-03 | 2010-11-23 | Honeywell International Inc. | Water removal downstream of a turbine |
GB2470151B (en) | 2008-03-05 | 2012-10-03 | Dresser Rand Co | Compressor assembly including separator and ejector pump |
BE1018075A3 (en) * | 2008-03-31 | 2010-04-06 | Atlas Copco Airpower Nv | METHOD FOR COOLING A LIQUID-INJECTION COMPRESSOR ELEMENT AND LIQUID-INJECTION COMPRESSOR ELEMENT FOR USING SUCH METHOD. |
US7922218B2 (en) | 2008-06-25 | 2011-04-12 | Dresser-Rand Company | Shear ring casing coupler device |
US8079805B2 (en) | 2008-06-25 | 2011-12-20 | Dresser-Rand Company | Rotary separator and shaft coupler for compressors |
US8062400B2 (en) | 2008-06-25 | 2011-11-22 | Dresser-Rand Company | Dual body drum for rotary separators |
US8210804B2 (en) | 2009-03-20 | 2012-07-03 | Dresser-Rand Company | Slidable cover for casing access port |
US8087901B2 (en) | 2009-03-20 | 2012-01-03 | Dresser-Rand Company | Fluid channeling device for back-to-back compressors |
US8061972B2 (en) | 2009-03-24 | 2011-11-22 | Dresser-Rand Company | High pressure casing access cover |
BR112012005866B1 (en) | 2009-09-15 | 2021-01-19 | Dresser-Rand Company | apparatus for separating a fluid and method for separating a component of higher specific weight from a component of lower specific weight of a fluid |
US20110097216A1 (en) * | 2009-10-22 | 2011-04-28 | Dresser-Rand Company | Lubrication system for subsea compressor |
EP2533905B1 (en) | 2010-02-10 | 2018-07-04 | Dresser-Rand Company | Separator fluid collector and method |
US8673159B2 (en) | 2010-07-15 | 2014-03-18 | Dresser-Rand Company | Enhanced in-line rotary separator |
US8663483B2 (en) | 2010-07-15 | 2014-03-04 | Dresser-Rand Company | Radial vane pack for rotary separators |
WO2012012018A2 (en) | 2010-07-20 | 2012-01-26 | Dresser-Rand Company | Combination of expansion and cooling to enhance separation |
WO2012012143A2 (en) | 2010-07-21 | 2012-01-26 | Dresser-Rand Company | Multiple modular in-line rotary separator bundle |
WO2012033632A1 (en) | 2010-09-09 | 2012-03-15 | Dresser-Rand Company | Flush-enabled controlled flow drain |
WO2013109235A2 (en) | 2010-12-30 | 2013-07-25 | Dresser-Rand Company | Method for on-line detection of resistance-to-ground faults in active magnetic bearing systems |
US8994237B2 (en) | 2010-12-30 | 2015-03-31 | Dresser-Rand Company | Method for on-line detection of liquid and potential for the occurrence of resistance to ground faults in active magnetic bearing systems |
US9551349B2 (en) | 2011-04-08 | 2017-01-24 | Dresser-Rand Company | Circulating dielectric oil cooling system for canned bearings and canned electronics |
WO2012166236A1 (en) | 2011-05-27 | 2012-12-06 | Dresser-Rand Company | Segmented coast-down bearing for magnetic bearing systems |
US8851756B2 (en) | 2011-06-29 | 2014-10-07 | Dresser-Rand Company | Whirl inhibiting coast-down bearing for magnetic bearing systems |
DE102011053634B3 (en) | 2011-09-15 | 2013-03-21 | Benteler Automobiltechnik Gmbh | Method and device for heating a precoated steel plate |
US10995995B2 (en) | 2014-06-10 | 2021-05-04 | Vmac Global Technology Inc. | Methods and apparatus for simultaneously cooling and separating a mixture of hot gas and liquid |
DE102016103554A1 (en) * | 2016-02-29 | 2017-08-31 | Karlsruher Institut für Technologie | Process for dissolving gases in liquids and apparatus for carrying it out |
JP6833172B2 (en) * | 2016-08-08 | 2021-02-24 | 三浦工業株式会社 | Heat recovery system |
JP6741196B2 (en) * | 2016-08-08 | 2020-08-19 | 三浦工業株式会社 | Air compression system |
DE202019101841U1 (en) * | 2019-04-01 | 2020-07-03 | Leybold Gmbh | Lubricant intake |
US11280247B2 (en) * | 2019-07-30 | 2022-03-22 | Vanair Manufacturing, Inc. | Pneumatic system and method for heating compressor oil and/or components of the system |
Citations (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2494644A (en) * | 1945-03-20 | 1950-01-17 | Dielectric Products Company In | Gas dehydration system |
US2955673A (en) * | 1958-08-18 | 1960-10-11 | Kahn And Company Inc | Process and apparatus for dehydrating gas |
US3226948A (en) * | 1964-10-07 | 1966-01-04 | Ingersoll Rand Co | Dehumidifying apparatus |
US4055403A (en) * | 1976-07-16 | 1977-10-25 | Whatman Reeve Angel Limited | Compressed air dryer |
US4375977A (en) * | 1981-01-23 | 1983-03-08 | Latoka Engineering, Inc. | System of gas dehydration using liquid desiccants |
US4406589A (en) * | 1980-02-29 | 1983-09-27 | Tokico Ltd. | Compressor |
US4553906A (en) * | 1983-09-28 | 1985-11-19 | Hydrovane Compressor Company Limited | Positive displacement rotary compressors |
US4642033A (en) * | 1984-11-19 | 1987-02-10 | The Hydrovane Compress Or Company Limited | Positive displacement air compressors |
US4898599A (en) * | 1989-05-12 | 1990-02-06 | Pneumatic Products Corporation | Desiccant gas drying system |
US5033944A (en) * | 1989-09-07 | 1991-07-23 | Unotech Corporation | Lubricant circuit for a compressor unit and process of circulating lubricant |
US5053126A (en) * | 1990-02-28 | 1991-10-01 | Ingersoll-Rand Company | Apparatus for gas liquid separation |
US5302300A (en) * | 1993-04-05 | 1994-04-12 | Ingersoll-Rand Company | Method and apparatus for separating water from a condensate mixture in a compressed air system |
US5487769A (en) * | 1994-09-27 | 1996-01-30 | Ingersoll-Rand Company | Integral apparatus for separating lubricant from a hot compressed gas and for cooling the separated lubricant |
US5492461A (en) * | 1992-02-14 | 1996-02-20 | Cash Engineering Research Pty. Ltd. | Separator vessel |
US5797980A (en) * | 1996-03-27 | 1998-08-25 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the treatment of atomospheric air |
US5993522A (en) * | 1998-05-13 | 1999-11-30 | Huang; Chin-Fu | Compressed air strainer and drying treatment |
US6156102A (en) * | 1998-11-10 | 2000-12-05 | Fantom Technologies Inc. | Method and apparatus for recovering water from air |
US6267560B1 (en) * | 1998-01-28 | 2001-07-31 | Institut Francais Du Petrole | Wet gas compression method with evaporation of the liquid |
US20030106431A1 (en) * | 2000-04-11 | 2003-06-12 | Kitchener Anthony John | Compressor/drier system and absorber therefor |
US6616719B1 (en) * | 2002-03-22 | 2003-09-09 | Yung Yung Sun | Air-liquid separating method and apparatus for compressed air |
Family Cites Families (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU1798546C (en) * | 1990-07-09 | 1993-02-28 | Омское научно-производственное объединение микрокриогенной техники "Микрокриогенмаш" | Compressor plant |
DE10196063B4 (en) * | 2000-04-11 | 2010-12-23 | Kitchener, Anthony John, North Melbourne | Integrated compressor dryer device |
-
2001
- 2001-04-10 DE DE10196063T patent/DE10196063B4/en not_active Expired - Fee Related
- 2001-04-10 WO PCT/AU2001/000403 patent/WO2001077528A1/en active IP Right Grant
- 2001-04-10 US US10/257,463 patent/US6843836B2/en not_active Expired - Lifetime
- 2001-04-10 JP JP2001574757A patent/JP4666871B2/en not_active Expired - Fee Related
Patent Citations (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2494644A (en) * | 1945-03-20 | 1950-01-17 | Dielectric Products Company In | Gas dehydration system |
US2955673A (en) * | 1958-08-18 | 1960-10-11 | Kahn And Company Inc | Process and apparatus for dehydrating gas |
US3226948A (en) * | 1964-10-07 | 1966-01-04 | Ingersoll Rand Co | Dehumidifying apparatus |
US4055403A (en) * | 1976-07-16 | 1977-10-25 | Whatman Reeve Angel Limited | Compressed air dryer |
US4406589A (en) * | 1980-02-29 | 1983-09-27 | Tokico Ltd. | Compressor |
US4375977A (en) * | 1981-01-23 | 1983-03-08 | Latoka Engineering, Inc. | System of gas dehydration using liquid desiccants |
US4553906A (en) * | 1983-09-28 | 1985-11-19 | Hydrovane Compressor Company Limited | Positive displacement rotary compressors |
US4642033A (en) * | 1984-11-19 | 1987-02-10 | The Hydrovane Compress Or Company Limited | Positive displacement air compressors |
US4898599A (en) * | 1989-05-12 | 1990-02-06 | Pneumatic Products Corporation | Desiccant gas drying system |
US5033944A (en) * | 1989-09-07 | 1991-07-23 | Unotech Corporation | Lubricant circuit for a compressor unit and process of circulating lubricant |
US5053126A (en) * | 1990-02-28 | 1991-10-01 | Ingersoll-Rand Company | Apparatus for gas liquid separation |
US5492461A (en) * | 1992-02-14 | 1996-02-20 | Cash Engineering Research Pty. Ltd. | Separator vessel |
US5302300A (en) * | 1993-04-05 | 1994-04-12 | Ingersoll-Rand Company | Method and apparatus for separating water from a condensate mixture in a compressed air system |
US5487769A (en) * | 1994-09-27 | 1996-01-30 | Ingersoll-Rand Company | Integral apparatus for separating lubricant from a hot compressed gas and for cooling the separated lubricant |
US5797980A (en) * | 1996-03-27 | 1998-08-25 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and installation for the treatment of atomospheric air |
US6267560B1 (en) * | 1998-01-28 | 2001-07-31 | Institut Francais Du Petrole | Wet gas compression method with evaporation of the liquid |
US5993522A (en) * | 1998-05-13 | 1999-11-30 | Huang; Chin-Fu | Compressed air strainer and drying treatment |
US6156102A (en) * | 1998-11-10 | 2000-12-05 | Fantom Technologies Inc. | Method and apparatus for recovering water from air |
US20030106431A1 (en) * | 2000-04-11 | 2003-06-12 | Kitchener Anthony John | Compressor/drier system and absorber therefor |
US6616719B1 (en) * | 2002-03-22 | 2003-09-09 | Yung Yung Sun | Air-liquid separating method and apparatus for compressed air |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20030106431A1 (en) * | 2000-04-11 | 2003-06-12 | Kitchener Anthony John | Compressor/drier system and absorber therefor |
US6843836B2 (en) * | 2000-04-11 | 2005-01-18 | Cash Engineering Research Pty Ltd. | Integrated compressor drier apparatus |
US6846348B2 (en) * | 2000-04-11 | 2005-01-25 | Cash Engineering Research Pty Ltd. | Compressor/drier system and absorber therefor |
US20050268781A1 (en) * | 2004-06-02 | 2005-12-08 | Rdc Research Llc | Method and system for processing natural gas using a rotary screw compressor |
US7377956B2 (en) * | 2004-06-02 | 2008-05-27 | Rdc Research Llc | Method and system for processing natural gas using a rotary screw compressor |
US20110100213A1 (en) * | 2009-10-30 | 2011-05-05 | Matthias Finkenrath | System and method for reducing moisture in a compressed air energy storage system |
US8347629B2 (en) * | 2009-10-30 | 2013-01-08 | General Electric Company | System and method for reducing moisture in a compressed air energy storage system |
CN104801157A (en) * | 2015-04-08 | 2015-07-29 | 上海理工大学 | Moisture removal device and air compressor system |
US20170082098A1 (en) * | 2015-09-21 | 2017-03-23 | Clark Equipment Company | Condensate vaporization system |
US11649813B2 (en) * | 2015-09-21 | 2023-05-16 | Clark Equipment Company | Condensate vaporization system |
CN107983055A (en) * | 2017-12-18 | 2018-05-04 | 赵国庆 | A kind of environment-friendly boiler waste gas circulation cleaning equipment |
Also Published As
Publication number | Publication date |
---|---|
WO2001077528A1 (en) | 2001-10-18 |
DE10196063B4 (en) | 2010-12-23 |
US6843836B2 (en) | 2005-01-18 |
JP2003530519A (en) | 2003-10-14 |
DE10196063T1 (en) | 2003-03-13 |
JP4666871B2 (en) | 2011-04-06 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US6843836B2 (en) | Integrated compressor drier apparatus | |
MX2008006011A (en) | Multi-stage hybrid evaporative cooling system. | |
JP2008531965A (en) | Small heat pump using water as refrigerant | |
US9216378B2 (en) | Method for cool drying gas | |
EP1923123A2 (en) | Energy recovery system and method for a refrigerated dehumidification process | |
US5302300A (en) | Method and apparatus for separating water from a condensate mixture in a compressed air system | |
US20090126376A1 (en) | Oil Separation in a Cooling Circuit | |
US20170307251A1 (en) | Atmospheric water generator | |
US6865877B2 (en) | Compression feed for high humidity fuel gas | |
NO334581B1 (en) | Apparatus and method for simultaneously cooling and removing liquid from a gas from a compressor. | |
US4267705A (en) | Refrigeration purging system | |
EP1946819B1 (en) | Pre-emptive air dryer control in a compressed air system | |
EP0031971B1 (en) | Close-circuit condensation depurator of gaseous flows containing solvents | |
AU2001248141B2 (en) | Integrated compressor drier apparatus | |
US6846348B2 (en) | Compressor/drier system and absorber therefor | |
RU2733843C1 (en) | Device and method of wet compressed gas drying and compressor plant containing such device | |
RU2336434C2 (en) | Gas compression system | |
AU2001248140B2 (en) | Compressor/drier system and absorber therefor | |
JPH06200729A (en) | Ga-liquid separating device | |
AU2001248140A1 (en) | Compressor/drier system and absorber therefor | |
JPH0498058A (en) | Recovering, regenerating and charging device for refrigerant | |
CS224091B1 (en) | Equipment for drying of gas by cooling |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: CASH ENGINEERING RESEARCH PTY LTD., AUSTRALIA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:KITCHENER, ANTHONY JOHN;REEL/FRAME:013491/0320 Effective date: 20021007 |
|
STCF | Information on status: patent grant |
Free format text: PATENTED CASE |
|
AS | Assignment |
Owner name: KITCHENER, ANTHONY JOHN, AUSTRALIA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:CASH ENGINEERING RESEARCH PTY. LTD.;REEL/FRAME:017846/0750 Effective date: 20060124 |
|
FPAY | Fee payment |
Year of fee payment: 4 |
|
AS | Assignment |
Owner name: SULLAIR CORPORATION,INDIANA Free format text: NUNC PRO TUNC ASSIGNMENT;ASSIGNOR:KITCHENER, ANTHONY JOHN;REEL/FRAME:024305/0186 Effective date: 20100424 |
|
FPAY | Fee payment |
Year of fee payment: 8 |
|
AS | Assignment |
Owner name: SULLAIR, LLC, INDIANA Free format text: CONVERSION OF CORPORATION TO LLC;ASSIGNOR:SULLAIR CORPORATION;REEL/FRAME:029388/0676 Effective date: 20121129 |
|
AS | Assignment |
Owner name: DEUTSCHE BANK AG NEW YORK BRANCH, AS COLLATERAL AG Free format text: SECURITY AGREEMENT;ASSIGNOR:SULLAIR, LLC;REEL/FRAME:029530/0607 Effective date: 20121213 |
|
FPAY | Fee payment |
Year of fee payment: 12 |
|
AS | Assignment |
Owner name: SULLAIR, LLC, INDIANA Free format text: TERMINATION AND RELEASE OF SECURITY INTEREST IN PATENTS (RELEASES RF 029530/0607);ASSIGNOR:DEUTSCHE BANK AG NEW YORK BRANCH,;REEL/FRAME:043177/0113 Effective date: 20170712 |